Manufacturing methods for the production of carbon materials

ABSTRACT

The present application is generally directed to activated carbon materials and methods for making the same. The disclosed methods comprise rapidly freezing synthetically prepared polymer gel particles. The methods further comprise drying, pyrolyzing, and activating steps to obtain an activated carbon material of high porosity. The disclosed methods represent viable manufacturing processes for the preparation of activated carbon materials.

CROSS-REFERENCES TO RELATED APPLICATIONS

This application is a continuation of U.S. patent application Ser. No.12/756,668 filed on Apr. 8, 2010, now allowed, which claims the benefitunder 35 U.S.C. §119(e) of U.S. Provisional Patent Application No.61/167,814 filed on Apr. 8, 2009; and U.S. Provisional PatentApplication No. 61/219,344 filed on Jun. 22, 2009; both of which areincorporated herein by reference in their entireties.

STATEMENT OF GOVERNMENT INTEREST

Partial funding of the work described herein was provided by the U.S.Government under Contract No. W15P7T-09-C-5311 provided by theDepartment of Defense. The U.S. Government may have certain rights inthis invention.

BACKGROUND

1. Technical Field

The present invention generally relates to polymer gels, polymercryogels, activated carbon materials, and methods for making the same.

2. Description of the Related Art

Activated carbon is a highly porous form of elemental carbon, typicallyhaving a surface area of at least 500 m²/g. Activated carbon materialsare useful in many different applications. For example, activated carbonmaterials are used, inter alia, for chemical adsorption, gas storage,heterogeneous catalysis, and in energy storage devices. Given the broaddemonstrated utility of activated carbon materials, efficient methodsfor their production are needed in the art.

One traditional approach to produce high surface area activated carbonmaterials, such as for use in ultracapacitor electrodes and other energystorage devices, has been to pyrolyze an existing carbon-containingmaterial (e.g. coconut fibers or tire rubber). This results in a charwith relatively low surface area which can subsequently beover-activated to produce a material with the porosity necessary for thedesired application. Such an approach is inherently limited by theexisting structure of the precursor material. This approach alsotypically results in low process yields due to removal of a largeportion of the original char during the activation step.

Another approach for producing high surface area activated carbonmaterials has been to prepare a synthetic polymer from carbon-containingorganic building blocks (e.g. a polymer gel). As with the existingorganic materials, the synthetically prepared polymers are pyrolyzed andactivated to produce an activated carbon material. In contrast to thetraditional approach described above, the intrinsic porosity of thesynthetically prepared polymer results in higher process yields becauseless material is lost during the activation step. In addition, somecontrol over the pore size distribution of the final activated carbonmaterial can be exerted by using different building blocks and/orpolymerization conditions.

Although preparing activated carbon materials from synthetic polymershas several advantages over pyrolysis and activation of existingprecursor materials, the known methods have several disadvantages. Forexample, preparation of activated carbon materials from syntheticpolymers typically requires a time-consuming and expensive solventexchange step prior to supercritical drying or freeze drying.Furthermore, the dried polymer material (e.g. polymer cryogel oraerogel) typically contains a residual amount of organic solvent. Aviable manufacturing process for activated carbon materials mustovercome these and other limitations of the existing methods.

While significant advances have been made in the field of activatedcarbon materials, there continues to be a need in the art for new andimproved carbon materials and related methods. The present inventionfulfills these needs and provides further related advantages.

BRIEF SUMMARY

In general terms, the present invention is directed to activated carbonmaterials processes for preparing the same. In one embodiment, thedisclosure provides a method for making frozen polymer gel particlescomprising rapidly freezing polymer gel particles, wherein the polymergel particles have been generated from a polymer gel, and wherein thepolymer gel has been prepared by reaction of one or more polymerprecursers.

In another embodiment, the present disclosure provides a polymer cryogelcomprising less than about 1000 ppm of organic solvent.

In some embodiments, the present disclosure provides activated polymercryogel particles prepared according to the methods disclosed herein,wherein the activated polymer cryogel particles have a specific surfacearea of at least about 1000 m²/g.

In some embodiments, the present disclosure provides pyrolyzed polymercryogel particles prepared according to the methods disclosed herein,wherein the pyrolyzed polymer cryogel particles have a specific surfacearea of about 500 to about 800 m²/g.

These and other aspects of the invention will be apparent upon referenceto the attached drawings and following detailed description. To thisend, various references are set forth herein which describe in moredetail certain procedures, compounds and/or compositions, and are herebyincorporated by reference in their entirety.

BRIEF DESCRIPTION OF THE DRAWINGS

In the figures, identical reference numbers identify similar elements.The sizes and relative positions of elements in the figures are notnecessarily drawn to scale and some of these elements are arbitrarilyenlarged and positioned to improve figure legibility. Further, theparticular shapes of the elements as drawn are not intended to conveyany information regarding the actual shape of the particular elements,and have been solely selected for ease of recognition in the figures.

FIG. 1 shows a differential scanning calorimetry scan for a polymerhydrogel.

FIG. 2 shows a vapor pressure of ice curve.

FIG. 3A shows four interaction plots for RC (reactant to catalyst molarratio) and RW (reactant to water molar ratio) using the Taguchi L12approach with BET surface area as a response.

FIG. 3B shows four interaction plots for RW and activation temperatureusing the Taguchi L12 approach with BET surface area as a response.

FIG. 3C shows four interaction plots for pyrolysis time and RW using theTaguchi L12 approach with BET surface area as a response.

FIG. 4 depicts representative pore size distribution for a cryogel(dashed line) and for an activated carbon (solid line).

FIG. 5 depicts pore size distribution in an activated carbon fordifferent levels of activation. The solid line is the case of loweractivation (i.e., shorter dwell time) compared to the dashed linerepresenting the case of higher activation (e.g., longer dwell time).

FIG. 6 presents BET specific surface area versus activation weight lossunder CO₂ for various samples, as described in Table 1 as indicated inthe legend.

FIG. 7 presents the surface area as a function of pore size foractivated carbon (representing Run #14 from Table 1).

FIG. 8 presents the surface area of pores between 0.5 and 0.6 nm inrelation to total measured BET surface area for an activated carbon.

FIG. 9A is a graph of surface area as a function of pore size foractivated carbon prepared from cryogel that was pyrolyzed at a dwelltime of 60 min at 1200° C. under nitrogen gas flow conditions andsubsequently activated for a dwell time of 10 min at 900° C. under CO₂gas flow conditions.

FIG. 9B is a graph of surface area as a function of pore size foractivated carbon prepared from cryogel as described in FIG. 7A, exceptthe activated carbon sample was further activated for a dwell time of anadditional 4 min at 900° C. under CO₂ gas flow conditions.

FIG. 9C is a graph of surface area as a function of pore size foractivated carbon prepared from a cryogel that was pyrolyzed at a dwelltime of 60 min at 900° C. under nitrogen gas flow and directly subjectedto activation for a dwell time of 14 min at 900° C. under CO₂ flowconditions.

FIG. 10 is a graph of tap density vs. specific surface area for variouslyophilized polymer gels (data from Table 6).

FIG. 11 is a graph of specific surface area vs. lyophilization chamberpressure for various lyophilized polymer gels (data from Table 6).

FIG. 12 is a differential scanning calorimetry scan for a polymerhydrogel.

DETAILED DESCRIPTION

In the following description, certain specific details are set forth inorder to provide a thorough understanding of various embodiments.However, one skilled in the art will understand that the invention maybe practiced without these details. In other instances, well-knownstructures have not been shown or described in detail to avoidunnecessarily obscuring descriptions of the embodiments. Unless thecontext requires otherwise, throughout the specification and claimswhich follow, the word “comprise” and variations thereof, such as,“comprises” and “comprising” are to be construed in an open, inclusivesense, that is, as “including, but not limited to.” Further, headingsprovided herein are for convenience only and do not interpret the scopeor meaning of the claimed invention.

Reference throughout this specification to “one embodiment” or “anembodiment” means that a particular feature, structure or characteristicdescribed in connection with the embodiment is included in at least oneembodiment. Thus, the appearances of the phrases “in one embodiment” or“in an embodiment” in various places throughout this specification arenot necessarily all referring to the same embodiment. Furthermore, theparticular features, structures, or characteristics may be combined inany suitable manner in one or more embodiments. Also, as used in thisspecification and the appended claims, the singular forms “a,” “an,” and“the” include plural referents unless the content clearly dictatesotherwise. It should also be noted that the term “or” is generallyemployed in its sense including “and/or” unless the content clearlydictates otherwise.

DEFINITIONS

As used herein, and unless the context dictates otherwise, the followingterms have the meanings as specified below.

The term “polymer” refers to a substance composed of macromolecules.Polymers are generally composed of monomer building blocks.

The term “monolithic” refers to a solid, three-dimensional structurethat is not particulate in nature.

As used herein the term “sol” refers to a colloidal suspension ofprecursor particles (e.g. monomer building blocks), and the term “gel”refers to a wet three-dimensional porous network obtained bycondensation or reaction of the precursor particles.

As used herein the term “polymer gel” refers to gel in which the networkcomponent is a gel; generally a polymer gel is a wet (aqueous ornon-aqueous based) three-dimensional structure comprised of a polymerformed from synthetic precursors or monomer building blocks.

As used herein the term “sol gel” refers to a sub-class of polymer gelwhere the polymer is a colloidal suspension that forms a wetthree-dimensional porous network obtained by condensation of theprecursor particles.

As used herein the term “polymer hydrogel” or “hydrogel” refers to asubclass of polymer gel wherein the solvent for the synthetic precursorsor monomers is water or mixtures of water and one or more water-misciblesolvent.

As used herein the term “RF hydrogel” refers to a sub-class of polymergel wherein the polymer was formed from the catalyzed reaction ofresorcinol and formaldehyde in water.

As used herein the phrase “synthetic polymer precursor material” or“polymer precursor” refers to compounds used in the preparation of asynthetic polymer. Examples of precursor materials that can be used inthe preparation disclosed herein include, but are not limited toaldehydes (i.e. HC(═O)R, where R is an organic group), such as forexample, methanal (formaldehyde); ethanal (acetaldehyde); propanal(propionaldehyde); butanal (butyraldehyde); glucose; benzaldehyde;cinnamaldehyde, as well as phenolic compounds that can be react withformaldehyde or other aldehydes in the presence of a basic catalyst toprovide a polymeric gel (cross-linked gel).

As used herein, the phrase “dried polymer gel” refers to a polymer gelfrom which the solvent, generally water, or mixture of water and one ormore water-miscible solvent, has been removed.

The term “cryogel” refers to a gel that has been freeze dried.Analogously, a “polymer cryogel” is a polymer gel that has been freezedried. The term “cryogel”, includes cryogels as defined below.

A “pyrolyzed cryogel” or “pyrolyzed polymer cryogel” is a cryogel orpolymer cryogel that has been pyrolyzed but not yet activated.

An “activated cryogel” or “activated polymer cryogel” is a cryogel orpolymer cryogel, as defined herein, which has been activated toactivated carbon material.

The term “xerogel” refers to a polymer gel that is air dried, forexample at or slightly below atmospheric pressure and at or above roomtemperature.

The term “aerogel” refers to polymer gel that is dried by supercriticaldrying, for example using supercritical carbon dioxide.

As used herein, “organic extraction solvent” refers to an organicsolvent added to a polymer hydrogel after polymerization of the polymerhydrogel has begun, generally after polymerization of the polymerhydrogel is complete.

As used herein “rapid multi-directional freezing” refers to the processof freezing a polymer gel by creating polymer gel particles from amonolithic polymer gel, and subjecting said polymer gel particles to asuitably cold medium. The cold medium can be, for example, liquidnitrogen, nitrogen gas, or solid carbon dioxide. During rapidmulti-directional freezing nucleation of ice dominates over ice crystalgrowth. The suitably cold medium can be, for example, a gas, liquid, orsolid with a temperature below about −10° C. Alternatively, the suitablycold medium can be a gas, liquid, or solid with a temperature belowabout −20° C. Alternatively, the suitably cold medium can be a gas,liquid, or solid with a temperature below about −30° C.

As used herein, the terms “activate” and “activation” each refer to theprocess of heating a raw material or carbonized/pyrolyzed substance atan activation dwell temperature during exposure to oxidizing atmospheres(e.g. carbon dioxide, oxygen, or steam). The activation processgenerally results in a stripping away of the surface of the particles,resulting in an increased surface area. Alternatively, activation can beaccomplished by chemical means, for example, impregnation with chemicalssuch as acids like phosphoric acid or bases like potassium hydroxide,sodium hydroxide or salts like zinc chloride, followed by carbonization.

As used herein, the terms “carbonizing”, “pyrolyzing”, “carbonization”,and “pyrolysis” each refer to the process of heating a carbon-containingsubstance at a carbonization dwell temperature in an inert atmosphere(e.g. argon or nitrogen) or in a vacuum so that the targeted materialcollected at the end of the process is primarily carbon.

As used herein, “dwell temperature” refers to the temperature of thefurnace during the portion of a process which is reserved for neitherheating nor cooling, but maintaining a relatively constant temperature.For example, the carbonization dwell temperature refers to therelatively constant temperature of the furnace during carbonization, andthe activation dwell temperature refers to the relatively constanttemperature of the furnace during activation.

The term “pore” refers to an opening or depression in the surface, or atunnel in a carbon material, such as for example a cryogel, aerogel,xerogel or activated cryogel, activated aerogel or activated xerogel. Apore can be a single tunnel or connected to other tunnels in acontinuous network throughout the structure.

As used herein the term “pore structure” refers to the layout of thesurface of the internal pores within a carbon material, such as anactivated carbon. Components of the pore structure include pore size,pore volume, surface area, density, pore size distribution, and porelength. Generally the pore structure of activated carbon materialcomprises micropores and mesopores.

The term “mesopore” generally refers to pores having a diameter betweenabout 2 nanometers and about 50 nanometers. The term “micropore” refersto pores having a diameter less than about 2 nanometers.

The term “surface area” refers to the total specific surface area of asubstance measurable by the BET technique, typically expressed in unitsof m²/g. The BET (Brunauer/Emmett/Teller) technique employs an inertgas, usually nitrogen, to measure the amount of gas adsorbed on amaterial and is commonly used in the art to determine the accessiblesurface area of materials.

As used herein “connected” when used in reference to mesopores andmicropores refers to the spatial orientation of such pores.

As used herein “effective length” refers to the portion of the length ofthe pore that is of sufficient diameter such that it is available toaccept salt ions from the electrolyte.

As used herein the term “tunable” refers to an ability to adjust up ordown any one of pore size, pore volume, surface area, density, pore sizedistribution, and pore length of either or both of the mesopores andmicropores as well as other properties of the polymer hydrogel, polymergel, pyrolyzed polymer cryogel, or activated polymer cryogel. Tuning thepore structure can be accomplished a number of ways, including but notlimited to, varying parameters in the production of a polymer gel;varying parameters in the freeze-drying of the polymer gel; varyingparameters in the carbonizing of the dried polymer cryogel; and varyingthe parameters in the activation of the dried polymer cryogel as well asother techniques disclosed herein.

As noted above, in some embodiments of the present disclosure, a methodfor making frozen polymer gel particles is provided. The methodcomprises rapidly freezing polymer gel particles, wherein the polymergel particles have been generated from a polymer gel, and wherein thepolymer gel has been prepared by reaction of one or more polymerprecursers.

In further embodiments, of the above method, the method furthercomprises lyophilizing the frozen polymer gel particles to obtainpolymer cryogel particles.

In further embodiments, of the above method, the method furthercomprises pyrolyzing polymer cryogel particles to obtain pyrolyzedpolymer cryogel particles, wherein the polymer cryogel particles havebeen prepared by lyophilizing the frozen polymer gel particles.

In further embodiments, of the above method, the method furthercomprises activating pyrolyzed polymer cryogel particles to obtainactivated polymer cryogel particles, wherein the pyrolyzed polymercryogel has been prepared by pyrolyzing a polymer cryogel, and whereinthe polymer cryogel has been prepared by lyophilizing the frozen polymergel particles.

In further embodiments of the above method, rapidly freezing the polymergel particles comprises immersing the polymer gel particles in a liquidhaving a temperature below about −10° C. For example, in someembodiments, the liquid has a temperature below about −30° C.

In other further embodiments, the polymer gel particles are generated bygrinding or milling the polymer gel.

In other further embodiments, the liquid is liquid nitrogen.

In other further embodiments, the liquid is ethanol.

In other further embodiments, the polymer gel particles have an averageparticle size of less than about 30 mm. For example, in someembodiments, the polymer gel particles have an average particle size ofabout 0.5 mm to about 10 mm.

In other further embodiments, the polymer gel particles are immersed inthe liquid at a rate of about 5 grams/min.

In other further embodiments, rapidly freezing the polymer gel particlescomprises admixing the polymer gel particles with a cold solid. Forexample, in some further embodiments the gas is nitrogen.

In other further embodiments, rapidly freezing the polymer gel particlescomprises admixing the polymer gel particles with a gas having atemperature below about −10° C. For example, in some further embodimentsthe gas is liquid nitrogen.

In other further embodiments, the polymer gel particles are generated bygrinding or milling the polymer gel in the presence of a cold solid. Forexample, in some further embodiments, the cold solid is solid carbondioxide.

In other further embodiments, rapidly freezing the polymer gel particlescomprises contacting the polymer gel particles with an atomized liquidhaving a temperature below about −10° C. In some further embodiments,the atomized liquid has a temperature below about −30° C. In some otherfurther embodiments the atomized liquid is liquid nitrogen.

In other further embodiments, rapidly freezing the polymer gel particlescomprises contacting sprayed droplets comprising the polymer gelparticles with a cold medium having a temperature below about −10° C. toobtain frozen droplets comprising the frozen polymer gel particles. Forexample, in some embodiments, the cold medium has a temperature belowabout −30° C.

In other further embodiments of the above method, the sprayed dropletscomprise a suspension of the polymer gel particles.

In other further embodiments, the polymer gel particles comprise polymergel having a viscosity of less than about 1000 cP.

In other further embodiments, the sprayed droplets comprise polymer gelparticles comprising incompletely polymerized polymer gel. For example,in some further embodiments, polymerization of the polymer gel iscompleted after the sprayed droplets are contacted with the cold medium(i.e. after the freezing step). In other further embodiments, the frozendroplets are lyophilized to obtain freeze-dried particles and thepolymerization reaction is completed within the freeze-dried particle.In yet other further embodiments, polymerization of the polymer gel iscompleted within the frozen droplets.

In other further embodiments, the sprayed droplets further comprisemicrospheres comprising the polymer gel particles. For example, in somefurther embodiments, the microspheres comprise an emulsion selected froma water-in-oil (w/o) emulsion, oil-in-water (o/w) emulsion,oil-in-water-oil (o/w/o) emulsion, water-in-oil-in-water (w/o/w)emulsion, and water-in-oil-in-oil (w/o/o) emulsion. the emulsioncomprises a surfactant selected from non-ionic, cationic, non-ionicpolymeric, and non-ionic polymeric fluorinated surfactants.

In other further embodiments, the sprayed droplets are contacted withliquid nitrogen or ethanol having a temperature below about −30° C.

In other further embodiments, rapidly freezing the polymer gel particlescomprises rapidly puling a vacuum on the polymer gel particles.

In other further embodiments, the one or more polymer precursors areselected from phenolic compounds and aldehydes. For example, in somefurther embodiments, the one or more polymer precursors are selectedfrom resorcinol and formaldehyde.

In other further embodiments, preparing the polymer gel furthercomprises adding a basic catalyst to a mixture of resorcinol andformaldehyde. For example, some other further embodiments, the basiccatalyst is sodium carbonate. In yet other further embodiments, themolar ratio of resorcinol to catalyst is from about 50 to 1 to about 100to 1. In yet other further embodiments, the molar ratio of resorcinol tocatalyst is from about 25 to 1 to about 50 to 1.

In other further embodiments, water is added as a solvent to a mixtureof resorcinol and formaldehyde, and wherein the ratio of resorcinol towater is from about 0.05 to 1 to about 0.70 to 1. For example, infurther embodiments, the ratio of resorcinol to water is from about 0.15to 1 to about 0.35 to 1.

In other further embodiments, the polymer gel comprises less than about1000 ppm of organic solvent.

In other further embodiments of the above method, lyophilizing thefrozen polymer gel particles comprises placing the frozen polymer gelparticles in a lyophilizer having a shelf temperature of between about10° C. and about 25° C.

In other further embodiments, lyophilizing the frozen polymer gelparticles comprises placing the frozen polymer gel particles underreduced pressure of between about 50 mTorr and about 1000 torr.

In other further embodiments, pyrolyzing the polymer cryogel particlescomprises heating the polymer cryogel particles for between about 0 andabout 60 minutes.

In other further embodiments, pyrolyzing the polymer gel particlescomprises heating the polymer gel particles at temperatures from about700° C. to about 1200° C. For example in other further embodiments,pyrolyzing the polymer gel particles comprises heating the polymer gelparticles at temperatures from about 850° C. to about 1050° C.

In other further embodiments, activating the pyrolyzed polymer gelparticles comprises heating the pyrolyzed polymer gel particles forbetween about 1 minute and about 10 minutes.

In other further embodiments, activating the pyrolyzed polymer gelparticles comprises contacting the pyrolyzed polymer gel particles withan activating gas.

In other further embodiments, activating the pyrolyzed polymer gelparticles comprises heating the pyrolyzed polymer gel particles attemperatures from about 800° C. to about 1300° C. For example, In otherfurther embodiments, activating the pyrolyzed polymer gel particlescomprises heating the pyrolyzed polymer gel particles at temperaturesfrom about 900° C. to about 1050° C.

In other further embodiments, activating the pyrolyzed polymer gelparticles comprises activating the pyrolyzed polymer gel particles to adegree of activation from about 5% to about 90%.

In some embodiments, the present disclosure provides A polymer cryogelcomprising less than about 1000 ppm of organic solvent. For example, inother further embodiments the organic solvent is t-butanol. In anotherembodiment, the organic solvent is acetone

In other further embodiments, the polymer cryogel has a tap density ofbetween about 0.10 cc/g and about 0.60 cc/g. For example, in a furtherembodiment, the polymer cryogel has a tap density of between about 0.15cc/g and about 0.25 cc/g.

In other further embodiments, the polymer cryogel has a BET specificsurface area of between about 150 m²/g to about 700 m²/g. Alternatively,the polymer cryogel has a BET specific surface area of between about 400m²/g to about 700 m²/g.

In some embodiments, the present disclosure provides activated polymercryogel particles prepared according to the methods disclosed herein,wherein the activated polymer cryogel particles have a specific surfacearea of at least about 1000 m²/g.

In some embodiments, the present disclosure provides pyrolyzed polymercryogel particles prepared according to the methods disclosed herein,wherein the pyrolyzed polymer cryogel particles have a specific surfacearea of about 500 to about 800 m²/g.

In further embodiments, the pyrolyzed polymer cryogel particles have atap density of between about 0.40 cc/g and about 0.60 cc/g.

The activated carbon materials produced according to the methodsdisclosed herein can be used in applications requiring stable, highsurface area micro- and mesoporous structure including for example,ultracapacitor electrodes, solid-state gas storage, capacitivedeionization of salt water, biomedical applications including poisoncontrol and drug delivery, such as sustained drug delivery oflow-molecular weight and macromolecular drugs, tissue engineeringapplications including tissue scaffolding, air filtration, waterfiltration, catalytic convertors, and as carbon-based scaffold supportstructure for catalytic functions such as hydrogen storage or fuel cellelectrodes.

Rapid Freezing of Polymer Gels

Activated polymer cryogels may be prepared by the following steps:

1. Admixing appropriate precursors (e.g. resorcinol and formaldehyde ina 1:2 ratio) in stirred DI water and then adding catalyst (e.g. sodiumcarbonate) at room temperature.

2. The resulting sols are then sealed in glass ampoules or vials andgelled at 90° C. for at least 24 h or until gelation was complete.

3. The resulting hydrogels are then subjected to solvent exchange toreplace water with an organic solvent (e.g. tert-butanol) by rinsingthree times in fresh organic solvent for 24 h each time.

4. The solvent exchanged gels are then subsequently freeze dried (i.e.lyophilized) for 3 days.

5. The resulting cryogels are then pyrolyzed at set times andtemperatures

6. The polymer cryogels are then activated to produce an activatedcarbon material that could be used, for example, as an ultracapacitorelectrode.

The method described above suffers from several disadvantages. Forexample, the solvent exchange step is time consuming, expensive, andenvironmentally unfriendly. In addition, the resulting cryogel comprisesresidual amounts of the organic extraction solvent. A viablemanufacturing process must address these disadvantages.

Accordingly, in one embodiment, the present disclosure provides a methodof preparing polymer cryogels wherein the solvent exchange step iseliminated. Instead, the polymer gels are rapidly frozen and lyophilizedwithout undergoing solvent exchange. The resulting polymer cryogels aresubstantially free of organic extraction solvent, for example t-butanolor acetone.

As noted above, the processing techniques generally employed in theproduction of activated carbon are relatively inexpensive and scalable,with the exception of performing a solvent exchange of the aqueoussolvent for an organic solvent, such as t butanol prior tofreeze-drying. Solvent exchange has generally been used so that thedried material retains the pore structure built during the water-basedgelation process described herein. This exchange step is one variablethat contributes to the high mesoporosity of an activated carbonmaterial and correspondingly the high power performance demonstrated inultracapacitors using such an activated carbon.

Without being bound by theory, freeze-drying the polymer gel, as opposedto air-drying which is generally employed in the preparation ofxerogels, is thought to prevent or minimize capillary forces within thepores of the polymer. In the freeze-drying process, after the solventpresent in the polymer gel freezes, it is sublimated directly to a gasand no meniscus forms that could destroy the pore structure. An organicsolvent, such as t butanol or acetone, is routinely used as the solventduring freeze drying instead of water because of the difference in theexpansion coefficients of the solvents during freezing. When waterfreezes inside the pores of a polymer gel, the water expands as itbecomes solid and destroys the polymer network; t butanol can be easilyfrozen due to its near-room temperature freezing point (25° C.) and doesnot exert the same destructive pressure on the pore walls as thefreezing of water does. Unfortunately, t-butanol is expensive,potentially damaging to the environment, and generally a large volume ofit is needed to produce a solvent exchanged gel (the volume of solventused is approximately 10 times the volume of the gel being dried).

One approach used by the inventors to avoid the limitations associatedwith the use of t-butanol or other organic extraction solvents is toeliminate the step of solvent exchange of water for t butanol or otherorganic extraction solvents and directly freeze the water inside thepolymer gel quickly. The crystal structure of solid phase water takes upa larger volume than does the disorganized liquid phase. However, it ispossible to produce water in a solid state without allowing it tocrystallize and expand. If the temperature of water is reduced at a fastenough rate, the water molecules do not have time to organize into anordered crystal structure. The result is super-cooled water whichtransforms into an amorphous phase of solid, frozen water. Thecoefficient of expansion of this material relative to liquid water isnearly 1.0. So the structure of a polymer gel filled with “ice”(super-cooled water) of this type is subject to only very minimalfreezing stresses.

There are several approaches for inducing a super cooled state on watertrapped inside a small volume. Such techniques have been employed toinduce a super cooled state on the water in the pores of a polymer gelas disclosed herein. In one embodiment, super-cooling water in the poresof a polymer gel is performed by rapidly cooling small particles ofpolymer gel (having an average particle size of less than about 30 mm)by immersing them in a suitably cold liquid, for example, liquidnitrogen at −196° C. or ethanol cooled by dry ice. In anotherembodiment, the polymer gel is rapidly frozen by co-mingling or physicalmixing of polymer gel particles with a suitable cold solid, for example,dry ice (solid carbon dioxide. Another method is to use a blast freezerwith a metal plate at −60° C. to rapidly remove heat from the polymergel particles scattered over its surface. A third method of rapidlycooling water in a polymer gel particle is to snap freeze the particleby pulling a high vacuum very rapidly (the degree of vacuum is such thatthe temperature corresponding to the equilibrium vapor pressure allowsfor freezing). However, this method does not achieve the targeted verylow temperature of the material during the freezing step; for example,the temperature of the material prior to snap freezing may be close to0° C., and upon rapid exposure to a high vacuum the material remainsaround 0° C. Yet another method for rapid freezing comprises admixing apolymer gel with a suitably cold gas. In some embodiments the cold gasmay have a temperature below about −10° C. In some embodiments the coldgas may have a temperature below about −20° C. In some embodiments thecold gas may have a temperature below about −30° C. In yet otherembodiments, the gas may have a temperature of about −196° C. Forexample, in some embodiments, the gas is nitrogen.

In one embodiment, milled samples of polymer gel particles are loadedinto an appropriate freezer (blast or snap freezing) and frozen. Inanother embodiment, liquid nitrogen quenching is accomplished with aparticulate sample. For example, a sample to be quenched is added at arate of 5 g per minute to a 1-L bowl shaped Dewar containing liquidnitrogen, thereby allowing time for the sample to quench, freeze, andsink to the bottom of the bath. In another analogous embodiment, ethanolcooled by dry ice is used instead of liquid nitrogen. The milled polymergel particles may have a diameter prior to freezing of less than about30 mm, for example, between about 0.01 mm and about 25 mm; alternately,the average diameter of said polymer gel particles prior to freezing isbetween about 0.1 mm and about 10 mm, or about 0.7 mm and about 7 mm. Insome examples, the polymer gel particles are between about 2 mm andabout 5 mm.

The rapidly frozen particles may be collected using various approachesknown to those of skill in the art, for example by sedimentation, bycentrifugation, by containment in a permeable membrane, comprised of astainless steel or polymeric fiber mesh.

After collecting the rapidly frozen sample, they are transferred to astandard freezer for temporary storage. They are placed in the freezedryer within 48 hours in carefully timed batches to prevent occurrenceof a water phase transition from amorphous to crystalline ice. Afterremoval from the freeze dryer, samples can be stored under a nitrogenblanket in a closed container for long periods of time.

While it is not generally practical to process material that has toosmall of a particle size, particularly when dealing with large kilnswith controlled gas environments, as in the later pyrolysis/activationsteps, it is beneficial to the super cooling process to have smallparticles size. The cooling rate is an important variable in achieving asuper cooled state. Smaller particles cool quicker much the same waythat a droplet of water might freeze instantaneously whereas a fullglass takes many hours. For the snap freezing option, smaller particleswould also be better because there is more surface area available forevaporation/sublimation—both cooling processes—to occur. A finer meshsize has more surface area per pound of gel and hence cools faster whena vacuum is applied. The relationship between mesh size of the polymergel particles and the super cooling method is related to the mesoporevolume and can be optimized based on the approaches disclosed herein.

In some embodiments, the particles of polymer gel are solid particles.In other embodiments, the particles of polymer gel are suspended in asuitable liquid medium to form a suspension of polymer gel particles. Inyet other embodiments, the particles of polymer gel are solubilized in asuitable solvent. Examples of polymer gels that can be formulated assolutions or suspensions include but are not limited to polymer gelsprepared from resorcinol and formaldehyde, saccharide polymers such asstarch and dextran, poly(ethylene glycols), polyacrylates, polyamides,polyesters, polycarbonates, polyimides, and polystyrenes. The polymercan be in the form of a polymer or co-polymer, or mixture of polymers.The molecular weight of the polymer can be unimodal, bimodal, ormultimodal in character, or, for example, a mixture of polymers ofvarious molecular weights.

In some embodiments, atomized liquid nitrogen, as opposed to bulk liquidnitrogen, is used for rapidly freezing polymer gels. Atomized liquidnitrogen can be formed by various methods known in the art, for example,single-fluid and two-fluid atomization.

In some embodiments, atomized or bulk liquid nitrogen is used for sprayfreezing a polymer gel which is suspended in a sprayed droplet of asuitable fluid. The frozen spray is formed from liquid droplets havingan average diameter of less than 10,000 microns, less than 1000 microns,less than 100 microns, or even less than 10 microns.

In some embodiments, an atomized liquid is used for rapidly freezingsolid particles of polymer gel. For example, in some embodiments, theatomized liquid may have a temperature of less than about −10° C. Inother embodiments, the atomized liquid may have a temperature of lessthan about −20° C. In yet other embodiments, the atomized liquid mayhave a temperature of less than about −30° C. In other embodiments,atomized liquid nitrogen is used for rapidly freezing solid particles ofpolymer gel, as opposed to a bulk form (e.g., bulk solution or bulkmonolith). The frozen particles can be comprised of solid particleshaving an average diameter of less than 10,000 microns, less than 1000microns, less than 100 microns or even less than 10 microns. In otherembodiments, droplets comprised of multi-phasic systems, such assuspensions or emulsions, can also be rapidly frozen under theconditions disclosed herein

In another embodiment, the polymer gel particles are comprised of aviscous polymer gel, for example a polymer gel having a viscosity in therange of less than about 10 cP, or less than about 100 cP, or even lessthan about 1000 cP viscosity. The viscous polymer gel may be produced bya number of techniques known to those of skill in the art. For example,the viscous polymer gel may be comprised of a partially polymerized formof the polymer gel, and/or may be comprised of a relatively lowmolecular weight form of the polymerized polymer gel. Alternately, theviscous polymer gel may be formed at an elevated temperature, such asfor example, 80-100° C. In some embodiments, lower temperatures can beused in conjunction with an increase in gelation time. With sufficienttime, complete gelation can occur at temperatures as low as 20° C., sothe range of applicable temperatures is from 20-100° C., depending onthe time required for gelation. Alternately, gelation can occur attemperatures higher than 100° C. in a 100% humidity environment. In someembodiments, Temperatures up to 200° C. may be used. Such temperaturescan be achieved, for example, by the use of steam. The resulting polymergel is maintained at that elevated temperature during the atomizationstep described below.

The viscous polymer gel prepared as described above is atomized byvarious approaches known to those of skill in the art for atomizingviscous materials, for example, using high-pressure single-fluidatomization or two-fluid atomization, sonication nozzle atomization,spinning disk atomization, or electrostatic atomization. Followingatomization, droplets of the highly viscous polymer gel are frozenrapidly, for example by spray freezing, as described above (i.e. theatomized spray is contacted with a suitably cold medium, for example,liquid nitrogen or ethanol cooled by dry ice). For example, in someembodiments, the suitably cold medium may have a temperature of lessthan about −10° C. In other embodiments, the suitably cold medium mayhave a temperature of less than about −20° C. In yet other embodiments,the suitably cold medium may have a temperature of less than about −30°C. The rapidly frozen particles are then collected and the resulting iceformed therein is removed by sublimation. Sublimation of the ice isaccomplished by lyophilization under conditions suitable to maintain thefine ice crystal structure as described in more detail herein.

In another embodiment, the polymer gel is rapidly frozen beforepolymerization is complete. For example, droplets of aresorcinol/formaldehyde/sodium carbonate mixture may be rapidly frozen,for example by spray freezing. The rapidly frozen particles are thencollected, and polymerization of the mixture is completed within thefrozen particle. Analogously, droplets of aresorcinol/formaldehyde/sodium carbonate mixture in which polymerizationhas not yet been initiated may be rapidly frozen, for example by sprayfreezing. Polymerization may then be initiated and completed within therapidly frozen droplet.

Polymerization within the frozen particles may be accomplished using amethod other than heating, for example by microwave irradiation. Asdisclosed herein, the polymerization conditions can employ relativelylow temperatures, for example in the range of less than 100° C. or lessthan 50° C. over a relatively long time for example more than 1 day ormore than several days compared to conventional conditions wherepolymerization is accomplished at relatively high temperatures forexample above 50° C. or above 100° C. and for a relatively short time,for example, less than several days, preferably less than one day. Afterthe polymerization is deemed complete, the ice formed in the freezingprocess can be removed by sublimation, such as by lyophilization underconditions suitable to maintain the fine ice crystal structure asdescribed in more detail below.

In one embodiment, polymerization of resorcinol and formaldehyde orother polymer precursors can be started before the freezing step andcompleted in the frozen particle. In another embodiment, polymerizationof resorcinol and formaldehyde or other polymer precursors can bestarted before the freezing step and completed in the freeze driedparticle (i.e., after lyophilization). In yet another embodiment,polymerization of resorcinol and formaldehyde or other polymerprecursors can be started in the frozen particle (after freezing step iscompleted), and completed thereafter in the freeze-dried particle. Inyet another embodiment, polymerization of resorcinol and formaldehyde orother polymer precursors can be started and completed in the freezedried particle.

In yet another embodiment, the polymer gel particles may be comprised ofmicrospheres that are created by an emulsion approach, such as awater-in-oil (w/o) emulsion, oil-in-water (o/w) emulsion,oil-in-water-oil (o/w/o) emulsion, water-in-oil-in-water (w/o/w)emulsion, and water-in-oil-in-oil (w/o/o) emulsion. In suchmicrospheres, the aqueous phase may contain polymer precursors, forexample, resorcinol and formaldehyde, wherein the polymerization haseither not yet been initiated or has been initiated but not yetcompleted, and the organic phase can comprise an appropriate organicsolvent. Polymerization can be confined to the aqueous phase (within thew/o, w/o/w/ or w/o/o emulsion) comprising the polymer precursors. Suchmicrospheres can additionally contain surfactants, such as, but notlimited to nonionic (e.g. SPAN80), cationic (e.g.trimethylstearylammonium chloride, C18), nonionic polymeric fluorinated(e.g. FC4430), and nonionic polymeric surfactants. When nonionicsurfactants are present, the ratio of the emulsifiers to solvent, thetemperature of the emulsification and the holding time of theemulsification may all play a role in the properties of the resultingpolymer cryogel microspheres.

In another embodiment, a solution of polymer precursors, for example,resorcinol and formaldehyde, in which polymerization is not yetinitiated may be emulsified in an organic phase, for example to create aw/o emulsion. In yet another embodiment, a solution of polymerprecursors, for example, resorcinol and formaldehyde, in whichpolymerization is partially progressed is emulsified in an organicphase. Emulsification can be accomplished by various means known to theart including but not limited to high-speed mixing, sonication,homogenization (for example rotor stator homogenization), etc.Polymerization to yield a polymer gel is carried out under conditionsknown to those of skill in the art and as disclosed herein. Themicrospheres comprising polymer gel are harvested using methods familiarto those of skill in the art.

In these embodiments, the harvested microspheres are rapidly frozen, forexample by spray freezing. The spray freezing is accomplished bycontacting the atomized droplets of the w/o produced microspheres withatomized droplets of liquid nitrogen, or bulk liquid nitrogen, oranother suitably cold fluid, for example, ethanol in dry ice or ethanolcooled by another means. The w/o microspheres are frozen via sprayfreezing over a length of time that ranges from several seconds tosubstantially less than one second. Generally the w/o microspheres arefrozen via spray freezing over a period of substantially less than onesecond. The rapidly frozen w/o microspheres are collected by variousapproaches known to those of skill in the art, for example bysedimentation, by centrifugation, by containment in a permeablemembrane, for example comprised of a stainless steel or polymeric fibermesh, etc. Sublimation of ice from the collected microspheres isaccomplished by lyophilization under conditions suitable to maintain thefine ice crystal structure as described in more detail below.

Alternatively, the solution of polymer precursors, for example,resorcinol and formaldehyde, is emulsified in an organic phase, andfurther emulsified in a second organic phase to create a w/o/o emulsion.Emulsification to create the double emulsion can be carried out byvarious means known in the art, as described above. Polymerization isthen carried out under conditions known to those of skill in the art,and the microspheres harvested using methods disclosed herein. Themicrospheres are rapidly frozen, for example by spray freezing. Thespray freezing is accomplished by contacting the atomized droplets ofthe w/o/o produced microspheres with atomized droplets of liquidnitrogen, or bulk liquid nitrogen, or another suitably cold fluid, forexample, ethanol in dry ice or ethanol cooled by another means. Therapidly frozen w/o/o microspheres are collected and the ice formedduring the rapid freezing step is removed by sublimation. Sublimation ofice is accomplished by lyophilization under conditions suitable tomaintain the fine ice crystal structure as described in more detailbelow.

In another alternative embodiment, the solution of polymer precursors,for example, resorcinol and formaldehyde, is emulsified in an organicphase, for example, to create a w/o emulsion. Polymerization is thencarried out under conditions known to those of skill in the art, and themicrospheres are rapidly frozen, for example, by spray freezing into asecond organic phase, creating a w/o/o particle. Similar methodologiesas described above for spray freezing the single emulsion embodiment canalso be employed for spray freezing the w/o/o particle. In this case,the spray freezing is accomplished by contacting the atomized dropletsof the w/o produced microspheres with atomized droplets of liquid coldsecond organic phase, or contacting the atomized droplets with a coldbulk second organic phase. The rapidly frozen w/o/o particles arecollected and ice is removed by sublimation such as by lyophilizationunder conditions suitable to maintain the fine ice crystal structure asdescribed in more detail below.

In yet another embodiment, the solution of polymer precursors, forexample, resorcinol and formaldehyde, is emulsified in an organic phase,and further emulsified in a second aqueous phase to create a w/o/wemulsion. Similar methodologies as described above for spray freezingthe single emulsion embodiment and the w/o/w embodiment can also beemployed for spray freezing the w/o/w particle. Polymerization iscarried out under conditions known to those of skill in the art, and themicrospheres are harvested. The harvested microspheres are rapidlyfrozen, for example by spray freezing. The rapidly frozen w/o/wmicrospheres are collected and ice removed by lyophilization underconditions suitable to maintain the fine ice crystal structure asdescribed in more detail below.

In another embodiment of the present disclosure, spray freezing can beperformed on an aqueous or organic solution or suspension of a polymergel. Use of a pre-formed polymer obviates the need for a polymerizationstep in the process disclosed above since the starting material isalready polymeric. The solution or suspension can be atomized by methodsknown to those of skill in the art. The atomized material is thensubject to spray freezing. The rapidly frozen particles are collectedand the ice removed by sublimation such as lyophilization underconditions suitable to maintain the fine ice crystal structure asdescribed herein. In the case of an aqueous milieu, freeze drying isemployed to remove water ice, and in the case of an organic milieu,freezing drying or other suitable technique is employed to remove thefrozen crystals of the organic solvent.

The rapid freezing approaches described herein allow fine ice formationvia a high degree of nucleation with little time for crystal growth dueto the extremely rapid freezing rate. Without wishing to be bound bytheory, freezing models may be used to optimize freezing conditions. Forexample, consider a freezing model based on a steady-state heat transferphenomenon in which the heat is transported from the cold environment(Tc) through the freezing front (the frozen layer, dr, at a temperatureof Tf):

q=AK(Tf−Tc)/(R−r)

where Q is the heat transfer rate (J/sec), A is the surface area of thefreezing layer equal to 4π2, and K is thermal conductivity of thematrix, e.g., ice (˜2.2 watt m−1 K−1 at about 0° C.). Assuming that theheat transferred is consumed for water freezing into ice, and using ΔHthe latent heat of water freezing (3.34×105 J/kg), ρ the density ofwater (1000 kg/m3), ΔT=(Tf−Tc), and rearranging and integrating yields:

Θ=(ΔHρR2)/(2KΔT)

where Θ is the time to complete freezing, i.e., the “freezing time.”According to this model, for droplets of R=1, 10, and 100 m, freezingtime would be ˜4×10−7 s, ˜4×10−5 s, ˜4×10−3 s, respectively.

Thus, freezing time is proportional to length of material to freezesquared, or another way to look at it is that freezing rate isproportional to Θ-1 or length-2. For “classical” freeze drying, even“rapid” freezing from a lyophilized shelf would be on the order of 1-10sec, which allows for ice crystal growth. For the case where freezing isvery rapid, thus providing lots of ice nucleation but not much time forgrowth, calls for a product “thickness” for example no greater than 1000μm, or no greater than 100 μm, or no greater than 10 μm.

The melting point of water Tm (K) is lowered by confinement inside apore texture (for example that present in a polymer hydrogel) andrelated to the pore radius (nm) according to:

$r_{p} = {0.57 - \frac{65.7}{\left\lbrack {T_{m} - 273} \right\rbrack}}$

For example, water confined in a 10 nm pore melts at temperatures higherthan −7° C. The melting point drops to −14.5° C. when the pore radiusdecreases to 5 nm.

Preparation of Activated Carbon Materials

As noted above, in one embodiment of the present disclosure a method formaking frozen polymer gel particles is provided, wherein the methodcomprises rapidly freezing polymer gel particles, wherein the polymergel particles have been generated from a polymer gel, and wherein thepolymer gel has been prepared by reaction of one or more polymerprecursers.

In further embodiments, the present disclosure provides lyophilizing,pyrolizing, and activating methods. Details of the variable processparameters of the various embodiments of the disclosed methods aredescribed below.

A. Preparation of Polymer Gels

The polymer gel may be provided by co-polymerizing a first precursor anda second precursor in an appropriate solvent. In the case of a polymerhydrogel, the reaction is performed in an aqueous solution. The firstprecursor may be a phenolic compound and the second precursor may be analdehyde compound. The solvent may also further comprise a basiccatalyst. In one embodiment, of the method, the phenolic compound isresorcinol, catechol, hydroquinone, phloroglucinol, phenol, or acombination thereof; and the aldehyde compound is formaldehyde,acetaldehyde, propionaldehyde, butyraldehyde, benzaldehyde,cinnamaldehyde, or a combination thereof. In a further embodiment, thephenolic compound is resorcinol, phenol or a combination thereof, andthe aldehyde compound is formaldehyde. In one embodiment, the basiccatalyst is sodium carbonate, sodium bicarbonate, sodium hydroxide,lithium carbonate, lithium bicarbonate, lithium hydroxide, potassiumcarbonate, potassium bicarbonate, potassium hydroxide, berylliumcarbonate, beryllium bicarbonate, beryllium hydroxide, magnesiumcarbonate, magnesium carbonate, magnesium bicarbonate, magnesiumhydroxide, or a combination thereof. In another embodiment, the catalystis sodium carbonate, sodium bicarbonate, sodium hydroxide or acombination thereof. In a further embodiment, the catalyst is sodiumcarbonate.

In one embodiment of any of the methods described herein, beforefreezing, the polymer gel or polymer gel particles are rinsed withwater. In one embodiment, the average diameter of said polymer gelparticles prior to freezing is less than about 30 mm, for example,between about 0.01 mm and about 25 mm; alternately, the average diameterof said polymer gel particles prior to freezing is between about 0.1 mmand about 10 mm, or about 0.7 mm and about 7 mm. In some examples, thepolymer gel particles are between about 2 mm and about 5 mm. In furtherembodiments, the polymer gel particles are frozen via immersion in amedium having a temperature of below about −10° C., for example, belowabout −20° C., or alternatively below about −30° C. For example, themedium may be liquid nitrogen or ethanol in dry ice or ethanol cooled byanother means. In some embodiments, drying under vacuum comprisessubjecting the frozen particles to a vacuum pressure of below about 1400mTorr.

In another embodiment of the methods described herein, the molar ratioof resorcinol to catalyst is from about 10:1 to about 2000:1 or themolar ratio of resorcinol to catalyst is from about 20:1 to about 200:1.In further embodiments, the molar ratio of resorcinol to catalyst isfrom about 25:1 to about 100:1. In further embodiments, the molar ratioof resorcinol to catalyst is from about 25:1 to about 50:1. In furtherembodiments, the molar ratio of resorcinol to catalyst is from about100:1 to about 50:1.

In yet another embodiment of any of the aspects or variations describedherein, the polymer gel is essentially free of organic solvent (i.e.less than 1000 ppm of organic solvent). Generally, the organic solventis t-butanol or acetone. In one embodiment, the polymer gel containsless than 1000 ppm organic solvent, less than 100 ppm organic solvent,less than 10 ppm organic solvent, or less than 1 ppm organic solvent.

In yet another embodiment of any of the aspect or variations describedherein, the polymer gel is essentially free of organic extractionsolvent (i.e. less than 1000 ppm of organic extraction solvent).Generally, the organic extraction solvent is t-butanol or acetone. Inone embodiment, the polymer gel contains less than 1000 ppm organicextraction solvent, less than 100 ppm organic extraction solvent, lessthan 10 ppm organic extraction solvent, or less than 1 ppm organicextraction solvent.

Another embodiment of the present disclosure provides a polymer cryogelthat is essentially free of organic solvent (i.e. less than 1000 ppm oforganic solvent). Generally, the organic solvent is t-butanol oracetone. In one embodiment, the polymer cryogel contains less than 1000ppm organic solvent, less than 100 ppm organic solvent, less than 10 ppmorganic solvent, or less than 1 ppm organic solvent.

Another aspect of the present application is a polymer cryogel that isessentially free of organic extraction solvent (i.e. less than 1000 ppmof organic extraction solvent). Generally, the organic extractionsolvent is t-butanol or acetone. In one embodiment, the polymer cryogelcontains less than 1000 ppm organic extraction solvent, less than 100ppm organic extraction solvent, less than 10 ppm organic extractionsolvent, or less than 1 ppm organic extraction solvent.

In one embodiment, the polymer cryogel has a BET specific surface areaof 100 m²/g to about 1000 m²/g. Alternatively, the polymer cryogel has aBET specific surface area of between about 150 m²/g to about 700 m²/g.Alternatively, the polymer cryogel has a BET specific surface area ofbetween about 400 m²/g to about 700 m²/g.

In one embodiment, the polymer cryogel has a tap density of from about0.10 g/cc to about 0.60 g/cc. In one embodiment, the polymer cryogel hasa tap density of from about 0.15 g/cc to about 0.25 g/cc. In oneembodiment, the polymer cryogel has a specific surface area from about150 m²/g to about 700 m²/g. In one embodiment of any of the presentdisclosure, the polymer cryogel has a specific surface area of at leastabout 150 m²/g and a tap density of less than about 0.60 g/cc.Alternately, the polymer cryogel has a specific surface area of at leastabout 250 m²/g and a tap density of less than about 0.4 g/cc or aspecific surface area of at least about 500 m²/g and a tap density ofless than about 0.30 g/cc. In another embodiment of any of the aspectsor variations disclosed herein the polymer cryogel comprises a residualwater content of less than about 15%, less than about 13%, less thanabout 10% or less than about 5%.

Polymerization to form a polymer gel can be accomplished by variousmeans described in the art. For instance, polymerization can beaccomplished by incubating suitable synthetic polymer precursormaterials in the presence of a suitable catalyst for a period of time.The time for polymerization can be a period ranging from hours to days,depending on temperature (the higher the temperature the faster, thereaction rate, and correspondingly, the shorter the time required). Thepolymerization temperature can range from room temperature to atemperature approaching (but lower than) the boiling point of thestarting solution. For example, the temperature can range from about 20°C. to about 90° C. In the specific embodiment of resorcinol,formaldehyde and catalyst, the temperature can range from about 20° C.to about 100° C., typically from about 25° C. to about 90° C. In someembodiments, polymerization can be accomplished by incubation ofsuitable synthetic polymer precursor materials in the presence of acatalyst for 24 hours at about 90° C. Generally polymerization can beaccomplished between about 6 and about 24 hours at about 90° C., forexample between about 18 and about 24 hours at about 90° C.

The synthetic polymer precursor materials as disclosed herein include(a) alcohols, phenolic compounds, and other mono- or polyhydroxycompounds and (b) aldehydes, ketones, and combinations thereof.Representative alcohols in this context include straight chain andbranched, saturated and unsaturated alcohols. Suitable phenoliccompounds include polyhydroxy benzene, such as a dihydroxy or trihydroxybenzene. Representative polyhydroxy benzenes include resorcinol (i.e.,1,3-dihydroxy benzene), catechol, hydroquinone, and phloroglucinol.Mixtures of two or more polyhydroxy benzenes can also be used. Phenol(monohydroxy benzene) can also be used. Representative polyhydroxycompounds include sugars, such as glucose, and other polyols, such asmannitol. Aldehydes in this context include: straight chain saturatedaldeydes such as methanal (formaldehyde), ethanal (acetaldehyde),propanal (propionaldehyde), butanal (butyraldehyde), and the like;straight chain unsaturated aldehydes such as ethenone and other ketenes,2-propenal (acrylaldehyde), 2-butenal (crotonaldehyde), 3 butenal, andthe like; branched saturated and unsaturated aldehydes; andaromatic-type aldehydes such as benzaldehyde, salicylaldehyde,hydrocinnamaldehyde, and the like. Suitable ketones include: straightchain saturated ketones such as propanone and 2 butanone, and the like;straight chain unsaturated ketones such as propenone, 2 butenone, and3-butenone (methyl vinyl ketone) and the like; branched saturated andunsaturated ketones; and aromatic-type ketones such as methyl benzylketone (phenylacetone), ethyl benzyl ketone, and the like. The polymerprecursor materials can also be combinations of the precursors describedabove.

The relative amounts of alcohol-containing species (e.g. alcohols,phenolic compounds and mono- or poly-hydroxy compounds or combinationsthereof) reacted with the carbonyl containing species (e.g. aldehydes,ketones or combinations thereof) can vary substantially. In someembodiments, the ratio of alcohol-containing species to aldehyde speciesis selected so that the total moles of reactive alcohol groups in thealcohol-containing species is approximately the same as the total molesof reactive carbonyl groups in the aldehyde species. Similarly, theratio of alcohol-containing species to ketone species may be selected sothat the total moles of reactive alcohol groups in the alcoholcontaining species is approximately the same as the total moles ofreactive carbonyl groups in the ketone species. The same general 1:1molar ratio holds true when the carbonyl-containing species comprises acombination of an aldehyde species and a ketone species.

The total solids content in the aqueous solution prior to polymer gelformation can be varied. The weight ratio of resorcinol to water is fromabout 0.05 to 1 to about 0.70 to 1. Alternatively, the ratio ofresorcinol to water is from about 0.15 to 1 to about 0.6 to 1.Alternatively, the ratio of resorcinol to water is from about 0.15 to 1to about 0.35 to 1. Alternatively, the ratio of resorcinol to water isfrom about 0.25 to 1 to about 0.5 to 1. Alternatively, the ratio ofresorcinol to water is from about 0.3 to 1 to about 0.4 to 1.

Examples of solvents useful in the preparation of the activated carbonmaterial disclosed herein include but are not limited to water oralcohol such as, for example, ethanol, t butanol, methanol or mixturesof these, optionally further with water. Such solvents are useful fordissolution of the synthetic polymer precursor materials, for exampledissolution of the phenolic compound. In addition, in some processessuch solvents are employed for solvent exchange in the polymer gel(prior to freezing and drying), wherein the solvent from thepolymerization of the precursors, for example, resorcinol andformaldehyde, is exchanged for a pure alcohol. In one embodiment of thepresent application, a cryogel is prepared by a process that does notinclude solvent exchange.

Suitable catalysts in the preparation of polymer gels include basiccatalysts that facilitate polymerization of the precursor materials intoa monolithic polymer. Suitable catalysts include sodium salts such assodium carbonate, sodium bicarbonate, and sodium hydroxide. Relatedmono- and divalent salts can also be employed such as lithium carbonate,lithium bicarbonate, and lithium hydroxide, potassium carbonate,potassium bicarbonate, and potassium hydroxide, beryllium carbonate,beryllium bicarbonate, and beryllium hydroxide, magnesium carbonate,magnesium carbonate, magnesium bicarbonate, and magnesium hydroxide. Thecatalyst can also comprise various combinations of the catalystsdescribed above. Typically, such catalysts can be used in the range ofmolar ratios of 20:1 to 200:1 phenolic compound: catalyst. For example,such catalysts can be used in the range of molar ratios of 25:1 to 100:1phenolic compound: catalyst. In specific embodiments, the catalyst issodium carbonate.

B. Milling of Polymer Gels

A monolithic polymer gel can be physically disrupted to create smallerparticles according to various techniques known in the art. Theresultant polymer gel particles generally have an average diameter ofless than about 30 mm, for example, in the size range of about 1 mm toabout 25 mm, or between about 1 mm to about 5 mm or between about 0.5 mmto about 10 mm. Alternatively, the size of the polymer gel particles canbe in the range below about 1 mm, for example, in the size range ofabout 100 to 1000 microns. Techniques for creating polymer gel particlesfrom monolithic material include manual or machine disruption methods,such as sieving, grinding, milling, or combinations thereof. Suchmethods are well-known to those of skill in the art. Various types ofmills can be employed in this context such as roller, bead, and ballmills.

In a specific embodiment, a roller mill is employed. A roller mill hasthree stages to gradually reduce the size of the gel particles. Thepolymer gels are generally very brittle for a ‘wet’ material and are notdamp to the touch. Consequently they are easily milled using thisapproach, however, the width of each stage must be set appropriately toachieve the targeted final mesh. This adjustment is made and validatedfor each combination of gel recipe and mesh size. Each gel is milled viapassage through a sieve of known mesh size. Sieved particles can betemporarily stored in sealed containers.

Milling can be accomplished at room temperature according to methodswell known to those of skill in the art. Alternatively, milling can beaccomplished cryogenically, for example by co-milling the polymer gelwith solid carbon dioxide (dry ice) particles. In this embodiment, thetwo steps of (a) creating particles from the monolithic polymer gel and(b) rapid, multidirectional freezing of the polymer gel are accomplishedin a single process.

C. Rapid Freezing of Polymer Gels

After the polymer gel particles are formed from the monolithic polymergel, freezing of the polymer gel particles is accomplished rapidly andin a multi-directional fashion as described in more detail above.Freezing slowly and in a unidirectional fashion, for example by shelffreezing in a lyophilizer, results in dried material having a very lowsurface area as evidenced in an example herein. Similarly, snap freezing(i.e., freezing that is accomplished by rapidly cooling the polymer gelparticles by pulling a deep vacuum) also results in a dried materialhaving a low surface area. As disclosed herein rapid freezing in amultidirectional fashion can be accomplished by rapidly lowering thematerial temperature to at least about −10° C. or lower, for example,−20° C. or lower, or for example, to at least about −30° C. or lower.Rapid freezing of the polymer gel particles creates a fine ice crystalstructure within the particles due to widespread nucleation of icecrystals, but leaves little time for ice crystal growth. This provides ahigh specific surface area between the ice crystals and the hydrocarbonmatrix, which is necessarily excluded from the ice matrix.

D. Drying of Polymer Gels

In one embodiment, the frozen polymer gel particles containing a fineice matrix are lyophilized under conditions designed to avoid collapseof the material and to maintain fine surface structure and porosity inthe dried product. Details of the conditions of the lyophilization areprovided herein. Generally drying is accomplished under conditions wherethe temperature of the product is kept below a temperature that wouldotherwise result in collapse of the product pores, thereby enabling thedried material to retain an extremely high surface area.

One benefit of having an extremely high surface area in the driedproduct is the improved utility of the polymer cryogel for the purposeof fabrication of capacitors, energy storage devices, and otherenergy-related applications. Different polymer cryogel applicationsrequire variations in the pore size distribution such as differentlevels of micropore volume, mesopore volume, surface area, and poresize. By tuning the various processing parameters of the polymercryogel, high pore volumes can be reached at many different pore sizesdepending on the desired application.

The structure of the carbon is reflected in the structure of the polymercryogel which is in turn is established by the polymer gel properties.These features can be created in the polymer gel using a sol-gelprocessing approach as described herein, but if care is not taken inremoval of the solvent, then the structure is not preserved. It is ofinterest to both retain the original structure of the polymer gel andmodify its structure with ice crystal formation based on control of thefreezing process. In some embodiments, prior to drying the aqueouscontent of the polymer gel is in the range of about 50% to about 99%. Incertain embodiments, upon drying the aqueous content of the polymercryogel is than about 10%, alternately less than about 5% or less thanabout 2.5%.

Differential scanning calorimetry (DSC) data for a polymer hydrogeldemonstrates a large exothermic event at ˜−18° C. (see FIG. 1). Thesedata are consistent with freezing of water inside a pore of ˜4 nmradius. These findings indicate that the extremely rapid freezing forthe purposes of the current application not only constitutes a rapidfreezing rate, but also that the extent of the decrease is such that thematerial is brought below at least −18° C.

The DSC data also demonstrate that upon warming, there is a broad,complex endothermic behavior, with the onset about −13° C. and amidpoint of about −10° C. There appears to be a thermal transition atabout −2° C., and final melting at about +1° C. The various events maycorrespond to melting of different types of microstructures. The datasuggest that in order to avoid loss of fine product structure in thefrozen state, product temperature during initial (e.g., primary) dryingshould be maintained below −13° C. This is accomplished, for example, ina drying step where heat transfer during primary drying is dominated byconvection rather than conduction, thus the product temperature duringsublimation will correspond to the temperature of ice at equilibriumwith the chamber pressure.

FIG. 2 shows a vapor pressure if ice curve. Referring to FIG. 2, achamber pressure of about 2250 microns results in a primary dryingtemperature in the drying product of about −10° C. Drying at about 2250micron chamber pressure or lower case provides a product temperatureduring primary drying that is no greater than about −10° C. As a furtherillustration, a chamber pressure of about 1500 microns results in aprimary drying temperature in the drying product of about −15° C. Dryingat about 1500 micron chamber pressure or lower provides a producttemperature during primary drying that is no greater than about −15° C.As yet a further illustration, a chamber pressure of about 750 micronsresults in a primary drying temperature in the drying product of about−20° C. Drying at 750 micron chamber pressure or lower provides aproduct temperature during primary drying that is no greater than about−20° C. As yet a further illustration, a chamber pressure of about 300microns results in a primary drying temperature in the drying product ofabout −30° C. Drying at 300 micron chamber pressure or lower provides aproduct temperature during primary drying that is no greater than about−30° C.

E. Pyrolysis and Activation of Polymer Cryogels

The pyrolysis and activation of the freeze dried polymer cryogel can beaccomplished by methods described in the art and in more detail below.The porous structure of the resultant activated carbon is reflected inthe structure of the dried polymer cryogel, which is in turn establishedby the polymer gel properties. These features can be created in thepolymer gel using a sol-gel processing approach, but if care is nottaken during drying (e.g. removal of the solvent, often water), then thestructure is not preserved and the desired structural properties are nottranslated through the pyrolysis and activation processes.

As noted above, another embodiment of the present disclosure provides amethod for making an activated carbon material comprising pyrolysis andactivation of a cryogel disclosed herein. In some embodiments of thepresent disclosure, an activated carbon material having a specificsurface area of at least about 1000 m²/g is provided. Alternatively, theactivated carbon has a specific surface area of at least about 1500m²/g. Alternatively, the activated carbon has a specific surface area ofat least about 2000 m²/g. Alternately, the activated carbon has aspecific surface area of at least about 2500 m²/g. Alternately, theactivated carbon has a specific surface area of at least about 3000m²/g.

Generally, in the pyrolysis process, dried polymer cryogels are weighedand placed in a rotary kiln. The temperature ramp is set at 5° C. perminute, the dwell time and dwell temperature are set; cool down isdetermined by the natural cooling rate of the furnace. The entireprocess is usually run under an inert atmosphere, such as a nitrogenenvironment. Pyrolyzed samples are then removed and weighed. Otherpyrolysis processes are well known to those of skill in the art.

In some embodiments, pyrolysis dwell time (the period of time duringwhich the sample is at the desired temperature) is from about 0 minutesto about 120 minutes. In other embodiments, the dwell time is from about0 minutes to about 60 minutes. In other embodiments, the dwell time isfrom about 0 minutes to about 30 minutes. In yet other embodiments, thedwell time is from about 0 minutes to about 10 minutes.

In some embodiments, pyrolysis dwell temperature ranges from about 650°C. to 1800° C. In other embodiments pyrolysis dwell temperature rangesfrom about 700° C. to about 1200° C. In other embodiments pyrolysisdwell temperature ranges from about 850° C. to about 1050° C. In otherembodiments pyrolysis dwell temperature ranges from about 800° C. toabout 900° C.

Activation time and activation temperature both have a large impact onthe performance of the resulting activated carbon material, as well asthe manufacturing cost thereof. Increasing the activation temperatureand the activation dwell time results in higher activation percentages,which generally correspond to the removal of more material compared tolower temperatures and shorter dwell times. Higher activation oftenincreases performance of the final activated carbon, but it alsoincreases cost by reducing overall yield. Improving the level ofactivation corresponds to achieving a higher performance product at alower cost.

Pyrolyzed polymer gels may be activated by contacting the pyrolyzedpolymer gel with an activating agent. Many gases are suitable foractivating, for example gas which contains oxygen. Non-limiting examplesof activating gases comprise carbon dioxide, carbon monoxide, steam, andoxygen. Activating agents may also include corrosive chemicals. Otheractivating agents are known to those skilled in the art.

In some embodiments, the activation time is from about 1 minute to about48 hours. In other embodiments, the activation time is from about 1minute to about 24 hours. In other embodiments, the activation time isfrom about 5 minutes to about 24 hours. In other embodiments, theactivation time is from about 5 minutes to about 5 hours. In otherembodiments, the activation time is from about 5 minutes to about 1hour. In other embodiments, the activation time is from about 5 minutesto about 10 minutes. In other embodiments, the activation time is fromabout 1 minute to about 10 minutes.

Generally, in the activation process, samples are weighed and placed ina rotary kiln, for which the automated gas control manifold is set toramp at a 20° C. per minute rate. Carbon dioxide is introduced to thekiln environment for a period of time once the proper activationtemperature has been reached. After activation has occurred, the carbondioxide is replaced by nitrogen and the kiln is cooled down. Samples areweighed at the end of the process to assess the level of activation.Other activation processes are well known to those of skill in the art.In some of the embodiments disclosed herein, activation temperatures mayrange from about 800° C. to about 1300° C. In another embodiment,activation temperatures may range from about 900° C. to about 1050° C.In another embodiment, activation temperatures may range from about 900°C. to about 1000°. One skilled in the art will recognize that otheractivation temperatures, either lower or higher, may be employed.

The degree of activation is measured in terms of the mass percent of thepyrolyzed cryogel that is lost during the activation step. In oneembodiment of the methods described herein, activating comprises adegree of activation from about 5% to about 90%; or a degree ofactivation from about 10% to about 80%; in some cases activatingcomprises a degree of activation from about 40% to about 70%, or adegree of activation from about 50% to about 60%.

In the methods disclosed herein for the production of high surface areaactivated carbon materials, the polymer gel is engineered to produce amaterial which is already highly porous and contains within its polymerframework a carbonic structure which, when pyrolyzed and activated, willproduce an activated carbon that contains a targeted mix of mesoporesand micropores. By producing polymer gel with the appropriate targetedmix of meso- and micro-pores, the amount of required activation isreduced, thereby improving yield and reducing cost. Also, the ability totune the properties (e.g. pore size) of the intermediates introduces adegree of tuneability that has not been realized by a more traditionalapproach of pyrolyzing and over-activating existing carbon material. Forexample, manipulating the processing variables of the intermediates asdescribed herein has a more important impact on the final carbonnanostructure than the traditional methods of adjusting pyrolysis andactivation variables.

The ability to scale up a manufacturing approach as disclosed herein tomeet the high demand expected for the activated carbon materialsdisclosed herein has been demonstrated. Three parts of the process canbe identified: 1) polymerization from precursor polymer materials; 2)freeze drying; and 3) pyrolysis/activation. In one embodiment, each ofthese steps may be scaled employing standard manufacturing equipment ofthree existing industries, for example, specialty chemical companiesworking with adhesives and epoxies; pharmaceutical and food relatedfreeze drying providers; and manufactures of low grade activated carbon,respectively.

It has been shown that the amount of catalyst and percentage of water inthe initial sol has a significant impact on the final performance of theactivated carbon material (e.g. when used in a supercapacitor). Thelarge number of process variables and the interaction between thesevariables enables continuous refinement of the process and allows forsome control over the final carbon structure. Accordingly, in oneembodiment, the present disclosure provides refinement of the processvariables. The disclosed refinements result in an ability to exertcontrol over the final carbon structure in a manner that was previouslyunobtainable.

The most common approach to refining process variables used in the artis to hold all but one variable constant and determine the effect ofvarying that one parameter. Alternately, and as described herein, thecombination of statistical analysis methods, DFE Pro Software, and afactorial design of experiments approach, were used to systematicallyvary multiple parameters simultaneously to obtain an optimized processfor preparing activated carbon material. By using this approach, theimpact of each of these variables on a range of different metrics (e.g.surface area, density, pore volume, etc.) related to the activatedcarbon material's structure are evaluated. When the activated carbonmaterial is employed in a supercapacitor, additional performance metricsmay be evaluated. For example, capacitance, density and power densitymay be evaluated.

FIG. 3 provides a representative sample of three of the variables whichhave strong, moderate and low interactions. FIG. 3A shows theinteraction between RC (resorcinol to catalyst ratio) and RW (resorcinolto water ratio). It is evident that under the appropriate experimentalconditions, for an RW of 0.125, the RC 50 value is better, but for an RWvalue of 0.25, the RC of 25 is better. This is considered a stronginteraction; the relationship between RC and RW and other variables canbe further controlled according to the approach disclosed herein.

FIG. 3B shows the moderate interaction between activation temperatureand RW. For low activation temperature, it appears better to have an RWof 0.25, but it also appears that this interaction is generally lessimportant because there is only a slight increase between the values.However, for an activation temperature of 900° C., it is important tochoose the lower RW value because there is a decrease in surface areawith an increase in RW.

FIG. 3C shows that there is essentially no interaction between RW andpyrolysis time: for either value of RW it is better to have the lowpyrolysis time. This variable interaction analysis provides a wealth ofinformation that can be used to optimize the performance of this systemto specific metrics. The ability to tune the pore size and otherproperties of an activated carbon material by refinement of all theprocess variables is disclosed in more detail below and in the examplesthat follow.

Characterization of Cryogels and Activated Carbon Materials

The structural properties of the final activated carbon material, thecarbon (e.g. resorcinol/formaldehyde) cryogels, and the pyrolyzed, butunactivated polymer cryogels are measured using Nitrogen sorption at17K, a method known to those of skill in the art. The final performanceand characteristics of the finished activated carbon material isimportant, but the intermediate products (both polymer cryogel andpyrolyzed, but not activated, polymer cryogel), can also be evaluated,particularly from a quality control standpoint, as known to those ofskill in the art. The Micromeretics ASAP 2020 is used to performdetailed micropore and mesopore analysis, which reveals the pore sizedistribution from 0.35 nm to 50 nm. The system produces a nitrogenisotherm starting at a pressure of 10−7 atm, which enables highresolution pore size distributions in the sub 1 nm range. The softwaregenerated reports utilize a Density Functional Theory (DFT) method tocalculate properties such as pore size distributions, surface areadistributions, total surface area, total pore volume, and pore volumewithin certain pore size ranges.

The pyrolyzed polymer cryogels may have a surface area from about 100 toabout 1200 m²/g. In other embodiments, the pyrolyzed polymer cryogelsmay have a surface area from about 500 to about 8000 m²/g. In otherembodiments, the pyrolyzed polymer cryogels may have a surface area fromabout 500 to about 600 m²/g.

The pyrolyzed polymer cryogels may have a tap density from about 0.1 toabout 1.0 cc/g. In other embodiments, the pyrolyzed polymer cryogels mayhave a tap density from about 0.4 to about 0.6 cc/g. In otherembodiments, the pyrolyzed polymer cryogels may have a tap density fromabout 0.45 to about 0.5 cc/g.

Tuning the Pore Size and Other Properties of Polymer Cryogels

As noted above, activated polymer cryogels synthesized from synthetic,well-characterized precursors are different from activated carbon fromnatural sources such as coal, pitch, coconuts, etc. This is due in partto the fact that they can be tuned in both micropore and mesoporestructure and chemistry by carefully predesigned and executed processingcontrols. Additionally, an activated polymer cryogel as described hereincan contain a porous structure which can be optimized for a givenapplication (e.g. when used in a supercapacitor or other energy storagedevice). With the ability to tune the carbon nanostructure, performanceexceeding current performance data from traditional activated carbons isattained. Important variables include large accessible surface area,short micropores for electrolytic salt diffusion, and minimization ofwasted pore volume to enhance specific capacitance.

As noted above, manipulation of the process variables allows productionof activated carbons that have properties that suits the desiredapplication. Accordingly, in one embodiment a method of optimizing theprocess variables for production of polymer gels, polymer cryogels,pyrolyzed polymer cryogels and activated polymer cryogels is provided.As described in more detail in the examples that follow, one approachfor optimization of process parameters comprises a design of experimentsstrategy. Using this strategy, the influence of multiple processvariables (e.g. up to 8 variables) can be studied with relatively fewexperiments. The data obtained from the design of experiments can beused to manipulate process variables to obtain specific properties inthe polymer gels, polymer cryogels, and activated polymer cryogels. Forexample, in some embodiments, the process parameters which aremanipulated to obtain the desired product characteristics are selectedfrom: Resorcinol/Catalyst Ratio, Resorcinol/Water Ratio, Particle Sizeat Freezing Step, Quench Temperature, Pyrolysis Time, PyrolysisTemperature, Activation Temperature, and Activation Time andcombinations thereof.

EXAMPLES

The polymer gels, cryogels, pyrolyzed cryogels, and activated carbonmaterials disclosed in the following Examples were prepared according tothe methods disclosed herein. The following chemicals were used in theirpreparation: resorcinol (99+%, Sigma-Aldrich), formaldehyde solution(37%-stabilized with methanol, Fisher Scientific), sodium carbonate(99.5%, Sigma-Aldrich). The chemicals were used as received from thesupplier without further purification.

Unless indicated otherwise, the following conditions were generallyemployed. Resorcinol and formaldehyde were reacted in water in thepresence of a sodium carbonate catalyst. The molar ratio of resorcinolto formaldehyde was typically 0.5 to 1. The reaction was allowed toincubate in a sealed glass ampoule at 90° C. for at least 24 hours oruntil gelation was complete. The resulting polymer hydrogel containedwater, but no organic solvent; the polymer hydrogel was optionallywashed with water to remove unreacted precursors, but was not subjectedto solvent exchange of water for an organic solvent, such as t-butanol.The polymer hydrogel monolith was then physically disrupted, for exampleby milling, to form polymer hydrogel particles having an averagediameter of less than about 30 mm. Unless stated otherwise, theparticles were then rapidly frozen, generally by immersion in a coldfluid (e.g. liquid nitrogen or ethanol/dry ice) and lyophilized.Generally, the lyophilizer shelf was pre-cooled to −50° C. beforeloading a tray containing the frozen polymer hydrogel particles on thelyophilizer shelf. The chamber pressure for lyophilization was typicallyin the range of 50 to 1000 mTorr and the shelf temperature was in therange of +10 to +25° C. Alternatively, the shelf temperature can be setlower, for example in the range of 0 to +10 C. Alternatively, the shelftemperature can be set higher, for example in the range of 25 to +40 C.

The dried polymer hydrogel was typically pyrolyzed by heating in anitrogen atmosphere at temperatures ranging from 1000-1200° C. for aperiod of time as specified in the examples. Activation conditionsgenerally comprised heating a pyrolyzed polymer hydrogel in a CO₂atmosphere at temperatures ranging from 900-1000° C. for a period oftime as specified in the examples. Specific pyrolysis and activationconditions were as described in the following examples.

Example 1 Pore Size Distribution of Dried RF Cryogel and an ActivatedCarbon

FIG. 4 shows the pore size distribution of a representative RF cryogel(dashed line) and an activated carbon prepared from the same RF cryogel(solid line). FIG. 2 shows that the larger pores in the RF cryogel arecarried over to the resulting activated carbon. This behavior providesan opportunity to control the larger pores in the activated carbonmaterial through the chemistry and processing of the precursor gel. Thedata in FIG. 2 also demonstrate that the activation step opens themicroporosity and thus provides an opportunity for independent controlof this parameter.

FIG. 5 compares the pore size distribution for two activated carbonsthat were prepared from two different dried RF hydrogels. Specifically,the dashed curve represents data for an activated polymer cryogelprepared from a reaction solution having an RC of 50 and RW of 0.35, theresulting cryogel, which had a specific surface area of 603 m²/g, waspyrolyzed for 6 min at 1000° C. and activated for 30 min at 1000° C. Thetotal BET specific surface area for the resultant activated carbon was2186 m²/g.

The solid curve in FIG. 5 represents data for an activated polymercryogel prepared from a reaction solution having an RC of 50 and RW of0.15, the resulting cryogel, which had a specific surface area of 478m²/g, was pyrolyzed for 6 min at 1200° C. and activated for 8 min at900° C. The total BET specific surface area for the resultant activatedcarbon was 1116 m²/g. As shown in FIG. 5, activation conditions didsignificantly change the pore size distribution below 10 Å, but thedistribution slightly above 10 Å was enhanced by increased activation. Asimilar trend is observed for the sizes in the range of 20 to 40 Å.Accordingly, FIGS. 4 and 5 demonstrate that appropriate process controlcan tune the pore size distributions.

Example 2 Taguchi L-18 Experimental Design Program to Illustrate Controlof Product Characteristics Via Processing Parameters

A Taguchi L-18 experimental design program was executed to study thefollowing 8 factors relating to the processing of high surface areaactivated carbon from resorcinol-formaldehyde (RF) polymers:Resorcinol/Catalyst Ratio (“RC Ratio”: 3 levels), Resorcinol/Water Ratio(“RW Ratio”: three levels), Particle Size at Freezing Step (“SievingSize”: 3 levels), Quench Temperature (“Freezing Method”: 3 levels),Pyrolysis Time (2 levels), Pyrolysis Temperature (2 levels), ActivationTemperature (3 levels), and Activation Time (3 Levels). The specificexperimental plan as executed is presented in Table 1.

TABLE 1 Experimental parameters used to create a Taguchi L-18experimental design Pyrol- Pyrol- ysis ysis Act. Act. Run Time Temp TimeTemp RC RW Sieve Freeze # (Min) (C.) (Min) (C.) Ratio Ratio Size Method1 6 1000 5 900 25 0.15 1 A 2 6 1000 7.5 950 37.5 0.25 2 B 3 6 1000 101000 50 0.35 3 C 4 6 1100 5 900 37.5 0.25 3 C 5 6 1100 7.5 950 50 0.35 1A 6 6 1100 10 1000 25 0.15 2 B 7 6 1200 5 950 25 0.35 2 C 8 6 1200 7.51000 37.5 0.15 3 A 9 6 1200 10 900 50 0.25 1 B 10 60 1000 5 1000 50 0.252 A 11 60 1000 7.5 900 25 0.35 3 B 12 60 1000 10 950 37.5 0.15 1 C 13 601100 5 950 50 0.15 3 B 14 60 1100 7.5 1000 25 0.25 1 C 15 60 1100 10 90037.5 0.35 2 A 16 60 1200 5 1000 37.5 0.35 1 B 17 60 1200 7.5 900 50 0.152 C 18 60 1200 10 950 25 0.25 3 A Notes for Table 1: Factor 1 =pyrolysis time, Factor 2 = pyrolysis temperature, Factor 3 = activationtime, Factor 4 = activation temperature, Factor 5 = R/C, Factor 6 = R/W,Factor 7 = Sieving size (1 = 0.71 to 1 mm, 2 = 2-4.75 mm, 3 = 5.6-6.7mm), Factor 8 = freezing method (A = immersion in −30° C. ethanol, B =immersion in −77° C. ethanol, C = immersion in −196° C. liquidnitrogen).

The density of the RF hydrogel was measured by the immersion technique,known to those of skill in the art. The influence of the ratios ofResorcinol to Water (R/W) and Resorcinol to Catalyst (R/C) on the RFhydrogel density were examined. The R/W ratio was the dominantcontributor with a minor effect of higher density with increasingcatalyst, especially in the low water region. The cured gel densitycorrelated well with the gel water content as indicated by the totalweight loss on air drying. Additionally, the weight loss on freezedrying increased with the increasing water content of the initial gel.The weight loss for both air drying and lyophilization were inreasonable agreement, indicating that the freeze dry process waseffective in removing water.

The specific surface area of the freeze-dried gels was quitehigh—averaging 552 m²/gm. Without being bound by theory, it is expectedthat the surface area of the air-dried gels would be very low as aresult of pore collapse. The density measurement and air drying step canbe used as rapid predictors of the water removal required in the freezedrying step.

Pyrolysis was carried out in nitrogen at 1000° C., 1100° C. and 1200° C.for either 6 or 60 minutes. The average weight loss of the dry gel uponpyrolysis was 45.6 percent with a standard deviation of 1.20, indicatingthat the pyrolysis step can be completed at a relatively low temperaturein a short time. There was a general trend of increasing weight losswith time and temperature. Losses upon activation ranged from 30% to90%. These data demonstrate the balance achieved among product yield(i.e., activation weight loss) and activation temperature and dwelltime.

To demonstrate control over the activation weight loss, a Y bar marginalmeans plot was constructed for the eight different input variables atthree levels each (low, middle, high) as described in Table 2. Weightloss upon activation was chosen as the response parameter in thisexample because it is an indicator of the activated carbon surface area,as previously discussed. The regression analysis showed that the mostsignificant factors related to weight loss are activation time andactivation temperature.

TABLE 2 Screening factors and levels for the Y bar marginal means plotFACTOR A B C D G Pyrolysis Pyrolysis Activation Activation E F ParticleH Time Temp Time Temp R/C R/W Size Quench Low  6 min 1000 C. 5 min 900C. 25 0.15 Small −30 C. Medium NA 1100 C. 8 min 950 C. 37 0.25 Medium−60 C. High 60 min 1200 C. 10 min  1000 C.  50 0.35 Large −196 C. 

The ability to adjust the pore size distribution of the samples forpores smaller than 5 nm is related to the performance of the activatedcarbon for its intended utility, for example, use in electrodes forultracapacitors. These pore size distributions demonstrate an ability toadjust the pore volume in certain ranges. As a specific illustration,consider the incremental pore volume data for various activated carbonsgenerated as part of the Taguchi L-18 experimental design program. Thedashed line in FIG. 3 (representing Run #3 from Table 1) has a peak forpores having a width at just over 20 Angstroms as well as a peak forpores having a width just larger than 10 Angstroms. These pores are inthe size range that would be useful for ion penetration, such as in anultracapacitor. Other pore sizes will have alternative applications, forexample, for different sized ion penetration. These data illustrate howdifferent processing parameters provide different pore size distributionin the activated carbons, and depending on the particular pore size(s)required for a particular application, the process parameters can betuned to provide peak pore volumes in the desired peak pore sizes.

The amount of surface area of a carbon material measured by BET is aprimary indicator of its potential performance for a given application,for example as an electrode in a supercapacitor. In addition, theparameters of the activation step are the most important contributors tohigh surface area. For the present experiments, the carbon activationstep was conducted and evaluated at temperatures between 900° C. and1200° C. and under CO₂ exposure times of between about 6 and about 60minutes. The data indicate that a significant parameter relating to BETsurface area is the burn-off or weight loss in the activation step. FIG.6 is a summary of the activation versus BET results for a number ofsamples identified in Table 1.

Two general classes of activated RF materials were identified in thepresent experiments:

-   -   1. Materials that had high weight loss at short activation times        (40 to 50% in 5 to 10 minutes) relative to their BET surface        area. These materials in the lower portion of FIG. 4 are        inferior electrode candidates compared to other samples shown in        FIG. 4 because of their low BET surface area for a relatively        high activation weight loss. For example, Run #5 resulted in        materials with a specific surface area of only about 500 m²/g or        less after 60% activation weight loss, and only about 1500 m²/g        after about 80% weight loss.    -   2. Materials that had low weight loss at short activation times        (20 to 30% in 5 to 10 minutes) but developed relatively high        surface area (in the range of 1000 to 1500 m²/gm). For example        the lines corresponding to Run #17 and Run #3 represent        materials that achieve a surface area of at least about 2000        m²/gm with about 60% activation weight loss.

The micropore distributions for activated carbons produced according toseven of the initial Taguchi L18 design parameters were measured. FIG. 7shows a representative distribution curve for the surface area as afunction of pore size for a sample activated to 2186 m²/gm (Run #3 fromTable 1). FIG. 8 shows the relationship between surface area in therange between 5 and 6 Angstroms (0.5-0.6 nm) pore width vs. totalsurface area. These data demonstrate that as total surface areaincreases, the surface area of the range of pore width between 5-6Angstroms increases.

Activated carbon material produced from one of the compositions fromTable 1 (Run #17) was chosen for further evaluation. The results of thisstudy are depicted in FIG. 9A, FIG. 9B and FIG. 9C, which are graphs ofsurface area vs. pore size distribution for activated carbons made fromthe same dried polymer RF gels but activated under different processconditions as described below.

The curve shown in FIG. 9A corresponds to material pyrolyzed for 60 minat 1200° C. and activated for 10 min at 900° C. to yield a BET surfacearea of 1376 m²/gm. The typical large surface area peak between 0.5 and0.6 nm as depicted in FIG. 5 is also present in this sample. Inaddition, significant well-defined surface area peaks are present atpore sizes between 0.7 and 0.8 nm and also at 1.2 nm. Re-activation ofthis same sample to a BET surface area of 2106 m²/gm (curve shown inFIG. 9B) maintained the same peak distribution but uniformly increasedthe peak height over the entire size range.

In the case of the curve shown in FIG. 9C, the pyrolysis and activationconditions were modified as follows: pyrolysis for 60 min at 900° C.followed directly by in situ activation for 14 min at 900° C. Thisresulted in activation to 2930 m²/gm. The resulting surface area/poresize distribution was significantly changed from the earlier processingconditions. The peak heights at pore sizes 0.7 nm to 0.8 nm and at 1.2nm were higher, consistent with the increased total BET surface area.However, the peak centered at 5.5 nm disappeared and was replaced by twolarge peaks—one centered at 0.5 nm and the other at 0.59 nm.

Example 3 Control of Dried RF Hydrogel Characteristics and Drying Timeas a Function of Freeze Drying Variables

An RF hydrogel was prepared and sieved by hand to create polymerhydrogel particles as described below. The polymer hydrogel particleswere frozen by gradually dropping the material into a stainless steelbeaker containing liquid nitrogen. Once the entire sample was completelyfrozen, the frozen slurry of particles in liquid nitrogen was carefullypoured into an 8-inch pan, which had been pre-cooled with liquidnitrogen, and the pan was placed on a lyophilization shelf (typicallypre-cooled to at least −30° C.).

For each freeze drying run in which a combination of shelf temperatureand chamber pressure were tested, three samples were generated withdifferent loadings and sieving. Two thermocouples were placed withineach sample, with care taken to place thermocouples in the center,bottom of each sample, preferably without having the thermocoupledirectly contacting the pan. After the majority of liquid nitrogenboiled off from the samples loaded in the lyophilizer (as ascertained byvisual inspection), the lyophilizer doors were sealed and vacuum pumpstarted.

Samples were harvested after product thermocouples were within 2° C. ofthe lyophilizer shelf. For runs conducted at a shelf temperature of +10°C., the shelf was raised to +25° C. for at least an hour prior toharvest to avoid possible condensation on the dried product. For thepurpose of statistical modeling, drying time was defined as the time forall product thermocouples to reach at least within 2° C. of the shelftemperature. An alternate analysis was conducted using an alternativedefinition for drying time as the time for all product thermocouples toreach at least within 4° C. of the shelf temperature. The typicaloutputs (characteristics measured) were visual appearance (e.g., color)and low magnification stereomicroscopy, product yield (weight loss), tapdensity, and specific surface area.

A custom design of experiments (DOE) approach was employed to examinethe effect of various input factors on the output. The input factorsexamined were: sample loading/depth (two levels: 2 and 4 g/in²), gelparticle/sieving size (2 levels: 2000 microns and 4750 microns), shelftemperature setpoint (2 levels: 10° C. and 25° C.), and chamber pressuresetpoint (4 levels: 100, 300, 700, and 1000 mTorr). In general, theactual measured chamber pressures and shelf temperatures were close tothe intended setpoint. Additional runs were conducted in duplicate at achamber pressure setpoint of 50 mTorr and shelf temperature setpoint of+10° C. However, in this case, during the primary drying phase (firstseveral hours of drying) the actual measured pressure was higher thanthe intended setpoint, with a reading spiking to a level in the range of200-250 mTorr. A total of 11 runs are included herein, with threesamples per run and two thermocouples in each sample to provide a grandtotal of 66 data points for the statistical analysis. A summary of allsamples and drying data is provided in Table 3.

TABLE 3 Summary of Freeze Drying Data Shelf Siev- Time Time Temper-Chamber Product ing (h) to 2° (h) to 4° ature Pressure Loading Size C.of C. of Sample (° C.) (mTorr) (g/in²) (um) shelf shelf 015-1 10 50 24750  8.0 7.7  8.6 8.0 015-2 4 17.0 15.4 17.3 16.1 015-3 4 2000 18.117.4 18.9 17.8 016-1 10 50 2 4750  9.8 8.9  9.9 9.0 016-2 4 16.9 16.217.9 16.9 016-3 4 2000 17.6 17.1  18.5^(c) 17.7 008-1 10 100 2 4750  7.76.8  8.3 8.1 008-2  4^(d) 20.1 15.3 20.8 15.6 008-3 4 2000 13.8 13.015.4 14.2 006-1 10 300 2 4750 12.6 9.1 14.0 8.9 006-2 4 16.2 15.6 17.416.2 006-3 4 2000 14.2 13.1 15.8 15.1 005-1 10 700 2 4750 12.2 11.1 12.510.9 005-2 4 16.4 15.5 15.5 14.4 005-3 4 2000 13.4 13.2 13.3 12.9 007-110 1000 2 4750  8.8 8.1  9.9 8.2 007-2 4 16.3 15.9 16.5 16.1 007-3 42000 13.5 13.1 13.7 13.4 009-1 25 100 2 4750 12.1 7.4 12.7 7.5 009-2 413.8 12.7 14.0 12.9 009-3 4 2000 13.9 13.3 13.3 12.1 014-1 25 300 2 4750 8.7 5.8 10.4 5.9 014-2 4 13.0 11.5 13.0 12.1 014-3 4 2000 12.3 11.912.0 11.4 013-1 25 700 2 4750 10.5 6.9 11.1 7.2 013-2 4 12.3 10.8 12.411.3 013-3 4 2000 12.9 11.4 13.1 12.1 012-1 25 1000 2 4750 10.4 7.0 11.27.3 012-2 4 12.4 11.2 12.5 12.0 012-3 4 2000 11.9 10.9 11.6 10.3

The data for time to dry was modeled as a linear regression of the sumof the products of the various process inputs (product loading, sievingsize, shelf temperature, chamber pressure) and their fitted coefficientand p values. Table 4 presents a summary of the model for freeze dryingtime defined as time for product thermocouples to reach within 2° C. ofshelf. The model gave a reasonable fit with R²=0.6523 and F=28.6 (notethat according to the software, F>6 indicates a significant model forprediction). The model suggests that product load, shelf temperature,and chamber pressure are highly significant (p<0.05) in terms of theirinfluence on the output of drying time, and sieving size is somewhatsignificant (p=0.0606). Positive coefficients for product load andsieving size suggest that drying time increases when these variablesincrease. Negative coefficients for chamber pressure and shelftemperature suggest that drying time decreases when these variablesincrease.

TABLE 4 Summary of Model for Freeze Drying Time (to within 2° C. of theShelf) Name Coefficient P(2 Tail) Constant +11.979 8.8E−46 Productloading +2.584 5.1E−13 Shelf temperature −0.87483 0.0008 Chamberpressure −0.6798 0.0387 Sieving size +0.54091 0.0606

Table 5 presents a summary of the model for freeze drying time definedas time for product thermocouples to reach within 4° C. of shelf. Themodel gave a reasonable fit with R²=0.8648 and F=97 (note that accordingto the software, F>6 indicates a significant model for prediction). Themodel suggests that product load, and shelf temperature are highlysignificant (p<0.05) in terms of their influence on the output of dryingtime, and chamber pressure is somewhat significant (p=0.0543). Positivecoefficients for product load and sieving size suggest that drying timeincreases when these variables increase. Negative coefficients forchamber pressure and shelf temperature suggest that that drying timedecreases when these variables increase.

TABLE 5 Summary of Model for Freeze Drying Time (to within 4° C. of theShelf) Name Coefficient P(2 Tail) Constant +10.351 5.8E−52 Productloading +3.048 2.7E−23 Shelf temperature −1.319 7.6E−11 Chamber pressure−0.42906 0.0543 Sieving size +0.21818 0.2610

Therefore, both models provide a similar conclusion that to decreasedrying time, it is beneficial to maximize shelf temperature and chamberpressure, and minimize the sieving size and product load.

A summary of the characteristics of the various dried polymer gels isprovided in Table 6. The product yields were very consistent among thevarious samples, ranging from 78-81%, with an average of about 81%. Themeasured tap densities ranged from about 0.15 to about 0.27 cc/g(average=0.191 cc/g, standard deviation =0.032 cc/g). The varioussamples were analyzed for BET specific surface area. As the first stepin the procedure, the samples were de-gassed. The weight loss for thevarious samples upon degassing ranged from 2.5% to 12.3% (average=5.7%,standard deviation=2.1%). Presumably, this variability in weight lossupon degassing illustrated the variation in residual moisture in thevarious samples after freeze drying and storage prior to the BETanalysis. There is no obvious pattern between the weight loss upondegassing and other dried polymer gel characteristics or thelyophilization conditions tested.

A graph of the tap density vs. the specific surface area is presented inFIG. 10. The data show the general correlation that tap densitydecreases with increasing specific surface area (R²=0.74). Therelationship is logical considering that particles with higher specificsurface area (and correspondingly higher specific pore volume) will havea lower envelope density, which would translate into a lower tap densityfor a given dried particle size.

There was a general trend that higher product loading and lower sievingsize resulted in lower specific surface area. This trend is more evidentwhen analyzing a particular experiment (where chamber pressure and shelftemperature are fixed).

Comparison of the data for specific surface area and the chamberpressure revealed a dramatic relationship (FIG. 11). There iscorrelation that specific surface area of the lyophilized polymer geldecreases with increasing chamber pressure during lyophilization(R²=0.90). This finding demonstrates that, for a fixed polymer gelcomposition and fixed freezing method, control of the specific surfacearea in the dried polymer gel can be modulated by control of thelyophilization chamber pressure. This relationship can be rationalized,at least in part, by the concurrent observation that the producttemperature during the initial phase of drying (i.e., primary drying) isalso dependent on the chamber pressure; specifically, the lower thechamber pressure, generally the lower the product temperature duringprimary drying. A lower temperature during primary drying should alsominimize the opportunity for collapse of product porosity in the frozenstate, and hence provide higher surface area.

TABLE 6 Summary of Characterization of Freeze Dried Samples BET Wt. lossSpecific Shelf Chamber Product Sieving Tap on drying Surface TempPressure Loading Size Yield Density for BET Area Sample (° C.) (mTorr)(g/in²) (um) (%) (cc/g) (%) (m²/g) 015-1 10 50 2 4750 81 0.162 6.7 390;382 015-2 4 81 0.156 5.1 399 015-3 4 2000 81 0.166 5.8 379 016-1 10 50 24750 80 0.170 5.6 367 016-2 4 80 0.161 3.9 342 016-3 4 2000 80 0.19712.3  332 008-1 10 100 2 4750 81 0.151 5.2 365 008-2 4 81 0.158 3.7 349008-3 4 2000 ND 0.171 4.6 347 006-1 10 300 2 4750 81 0.168 8.6 323 006-24 81 0.180 4.3 303 006-3 4 2000 81 0.222 2.5 287 005-1 10 700 2 4750 780.220 5.7 250 005-2 4 80 0.222 3.8 246 005-3 4 2000 81 0.244 ND 213007-1 10 1000 2 4750 80 0.218 9.9 236 007-2 4 80 0.200 7.7 221 007-3 42000 81 0.274 6.1 183 009-1 25 100 2 4750 80 0.155 6.4 372 009-2 4 800.152 6.3 358 009-3 4 2000 81 0.211 3.9 347 014-1 25 300 2 4750 81 0.1608.0 357 014-2 4 81 0.170 5.0 353 014-3 4 2000 81 0.200 5.9 324 013-1 25700 2 4750 80 0.190 5.0 245 013-2 4 81 0.210 5.7 254 013-3 4 2000 810.240 5.7 250 012-1 25 1000 2 4750 81 0.155 5.1 215 012-2 4 81 0.152 2.3199 012-3  4s 2000 81 0.211 5.2 150

Example 4 Snap Freezing Followed by Lyophilization Results in LowSurface Area for RF Hydrogel

The RF hydrogel employed as the starting material in Example 3 was usedherein to compare freezing of polymer hydrogel particles via snapfreezing to freezing by immersion in liquid nitrogen. Snap freezing wasspecifically accomplished by placing RF hydrogel particles sievedbetween 4750 and 200 microns (that were precooled to 5° C.) in alyophilizer, and then immediately pulling a vacuum. The control samplewas the same RF hydrogel particles that had been frozen by immersion inliquid nitrogen, and dried under vacuum in the same experimental run atthe same lyophilization conditions of product loading, shelftemperature, and chamber pressure setpoints. A summary of the sample,the control, and the data for tap density and specific surface area forthe dried polymer hydrogel are given in Table 7.

TABLE 7 Summary of Samples and Data for Example 4. Specific ShelfChamber Product Sieving Tap Surface Temp. Pressure Loading Size DensityArea Freezing (° C.) (mTorr) (g/in²) (um) (g/cm³) (m²/g) Liquid nitrogenfreezing 10 50 4 4750 0.16 349 (control) Snap frozen 0.42 0.3

The data reveal that snap freezing results in very low specific surfacearea of the dried polymer cryogel, only about 0.3 m²/g. In contrast, thecontrol sample freeze dried in the same experiment exhibited a specificsurface area of 349 m²/g. It was also noted that the snap frozen samplewas very dense, exhibiting signs that “collapse” had occurred uponlyophilization. To provide a quantitative comparison, the tap density ofthe snap frozen sample was measured and was indeed much greater than thecontrol sample; 0.42 vs. 0.16 g/cm³, respectively.

This example illustrates that the relatively rapid freezing atrelatively high temperature provided by snap freezing was not capable ofyielding the high specific surface area that can be achieved by rapid,multidirectional freezing at very low temperature, for example, thataccomplished by immersion of RF hydrogel particles in liquid nitrogen.

Example 5 Differential Scanning Calorimetry of RF Hydrogel

The RF hydrogel of Example 3 was examined by differential scanningcalorimetry (DSC) to discern the nature of any thermal events occurringduring freezing. A representative thermogram is depicted in FIG. 12. Thedata show a large exothermic peak exhibited upon cooling atapproximately −18° C. This event suggests that in order to achievecomplete freezing of the material that the temperature must be broughtto at least this temperature or below. Upon warming, there was a complexbehavior seen, with several melting endotherms over the range of about−2 to +1 C, suggesting melting of different types of microstructures,and further supporting the conclusion that freezing drying conditionsshould be carefully selected to maintain fine product structure duringthe initial drying stage as discussed in more detail above.

The various embodiments described above can be combined to providefurther embodiments. All of the U.S. patents, U.S. patent applicationpublications, U.S. patent applications, foreign patents, foreign patentapplications and non-patent publications referred to in thisspecification and/or listed in the Application Data Sheet, areincorporated herein by reference, in their entirety. Aspects of theembodiments can be modified, if necessary to employ concepts of thevarious patents, applications and publications to provide yet furtherembodiments. These and other changes can be made to the embodiments inlight of the above-detailed description. In general, in the followingclaims, the terms used should not be construed to limit the claims tothe specific embodiments disclosed in the specification and the claims,but should be construed to include all possible embodiments along withthe full scope of equivalents to which such claims are entitled.Accordingly, the claims are not limited by the disclosure.

1-63. (canceled)
 64. A polymer cryogel comprising less than about 1000ppm of organic extraction solvent, wherein the polymer cryogel has a tapdensity ranging from about 0.10 g/cc to about 0.60 g/cc.
 65. The polymercryogel of claim 64, wherein the polymer cryogel has a BET specificsurface area ranging from about 100 m²/g to about 1000 m²/g.
 66. Thepolymer cryogel of claim 64, wherein the polymer cryogel has a BETspecific surface area of ranging from about 150 m²/g to about 700 m²/g.67. The polymer cryogel of claim 64, wherein the polymer cryogel has aBET specific surface area ranging from about 400 m²/g to about 700 m²/g.68. The polymer cryogel of claim 64, wherein the polymer cryogel has atap density ranging from about 0.15 g/cc to about 0.25 g/cc.
 69. Thepolymer cryogel of claim 66, wherein the polymer cryogel has a tapdensity ranging from about 0.15 g/cc to about 0.25 g/cc.
 70. The polymercryogel of claim 67, wherein the polymer cryogel has a tap densityranging from about 0.15 g/cc to about 0.25 g/cc.
 71. The polymer cryogelof claim 64, wherein the polymer cryogel comprises less than 100 ppm oforganic extraction solvent.
 72. The polymer cryogel of claim 64, whereinthe polymer cryogel comprises less than 10 ppm of organic extractionsolvent.
 73. The polymer cryogel of claim 64, wherein the organicextraction solvent is t-butanol.
 74. The polymer cryogel of claim 64,wherein the organic extraction solvent is acetone.